CN102319553B - Dimethyl ether synthesis reactor - Google Patents
Dimethyl ether synthesis reactor Download PDFInfo
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- CN102319553B CN102319553B CN201110252753.8A CN201110252753A CN102319553B CN 102319553 B CN102319553 B CN 102319553B CN 201110252753 A CN201110252753 A CN 201110252753A CN 102319553 B CN102319553 B CN 102319553B
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
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Abstract
The invention relates to a synthesis reactor, and especially relates to a reactor for dimethyl ether synthesis. The synthesis reactor comprises a tower type reactor and heat exchangers arranged in the tower type reactor. The synthesis reactor is characterized in that the tower type reactor therein is equipped with a water cooling heat exchanger and an air cooling heat exchanger from top to bottom; a separator is arranged on an upper end of the tower type reactor; an air intake is arranged on a lower end of the tower type reactor; a gas distributor is arranged between the air cooling heat exchanger and the air intake in the tower type reactor; a water inlet and a water outlet connected with the water cooling heat exchanger are arranged on the tower type reactor; a heat synthetic gas outlet and a cold synthetic gas inlet that are communicating with the air cooling heat exchanger are arranged from top to bottom on the tower type reactor; the heat synthetic gas outlet is communicating with the air intake arranged on the lower end of the tower type reactor through a pipeline. The synthesis reactor can increase CO single pass conversion and dimethyl ether selectivity, prolong catalyst life, recover energy reasonably, reduce production cost and enhance catalysis effect.
Description
Technical field
The present invention relates to a kind of synthesis reactor, particularly a kind of for the synthetic reactor of dimethyl ether.
Background technology
Mainly there is following problem in the reactor of synthesis of dimethyl ether with synthesis gas one-step at present: (1) is for fixed bed reactors, the thermal discharge of one-step method from syngas preparing dimethy ether is very large, heat cannot be removed in time, be caused catalytic bed excess Temperature, cause normal operating to carry out; (2), for gas-liquid-solid catalytic reactor, due to the existence of heat carrier, can keep bed reaction temperature, the heat that has solved one-step method from syngas preparing dimethy ether shifts out problem, can prevent that bed temperature is too high, but catalysqt deactivation is very fast, cannot guarantees process units long-term operation; (3) gas-solid catalytic reactor, due to the wearing and tearing of catalyst, catalyst loss is very fast, and operating cost is high, also cannot guarantee process units long-term operation.
Summary of the invention
The object of the invention is to overcome above-mentioned the deficiencies in the prior art, a kind of have rational Temperature Distribution and gradient are provided, catalyst distribution evenly, long service life, can effectively improve the selective of the conversion per pass of CO and dimethyl ether simultaneously, the dimethyl ether synthesis reactor that can reduce production costs.
For achieving the above object, technical scheme of the present invention is: a kind of dimethyl ether synthesis reactor, comprise tower reactor, be arranged on the heat exchanger in tower reactor, it is characterized in that being provided with the gentle cold heat exchanger of water cooling heat exchanger from top to bottom in tower reactor, in tower reactor upper end, separator is installed, in tower reactor lower end, air inlet is installed, in tower reactor, between air cooling heat exchanger and air inlet, gas distributor is installed, the water inlet and the delivery port that are connected with water cooling heat exchanger are installed on tower reactor, the hot synthesis gas outlet and the cold synthesis gas import that are connected with air cooling heat exchanger are from top to bottom installed on tower reactor, the air inlet that hot synthesis gas outlet is installed with tower reactor lower end by pipeline is connected.
Above-mentioned water cooling heat exchanger is comprised of the tubulation that is relatively arranged on two orifice plates in tower reactor and be arranged between two orifice plates, between two orifice plates, tubulation outer wall and tower reactor inwall form airtight heat exchange space, water inlet and delivery port from the bottom to top order are arranged on tower reactor, and are connected in heat exchange space.
Above-mentioned air cooling heat exchanger is comprised of the tubulation that is relatively arranged on two orifice plates in tower reactor and be arranged between two orifice plates, between two orifice plates, tubulation outer wall and tower reactor inwall form airtight air heat swapace, hot synthesis gas outlet and cold synthesis gas import are connected with air heat swapace.
Above-mentioned gas distributor is orifice plate, and the cylindrical of orifice plate is connected with tower reactor inwall is airtight.
In the tubulation of the gentle cold heat exchanger of above-mentioned water cooling heat exchanger, catalyst is housed.
Above-mentioned separator is spiral gas-liquid-solid separator.
Due to synthesis reactor of the present invention, utilize the heat release in synthetic reaction process, on the one hand the synthesis gas entering in reactor is heated, make to react liberated heat and can take away a part by the synthesis gas entering, utilize on the other hand water cooling heat exchanger and separator, rational Temperature Distribution and gradient in synthesis reactor, have been formed, catalyst granules is more evenly distributed at reaction bed, avoided that exit gas is liquid-solid to be carried secretly, improved the selective of the conversion per pass of CO and dimethyl ether, extended the life-span of catalyst, reasonably reclaimed energy, reduced production cost, the 3rd due in synthesis gas enters synthesis reactor, has increased the gas distributor of being made by orifice plate, makes like this to enter more all use that contacts of synthesis gas in synthesis reactor and catalyst, has improved catalytic effect.
Accompanying drawing explanation
Accompanying drawing 1 is structural representation of the present invention.
The specific embodiment
As shown in Figure 1, the gentle cold heat exchanger of water cooling heat exchanger is from top to bottom installed in tower reactor 1, in tower reactor upper end, separator 13 is installed, separator can adopt spiral gas-liquid-solid separator, in tower reactor lower end, air inlet 9 is installed, air inlet also can be used as catalyst removal mouth.
Above-mentioned water cooling heat exchanger is comprised of the tubulation 2 that is relatively arranged on two orifice plates 4 in tower reactor 1 and be arranged between two orifice plates, between two orifice plates, tubulation outer wall and tower reactor inwall form airtight heat exchange space 3, water inlet 11 and delivery port 12 from the bottom to top order are arranged on tower reactor, and are connected in heat exchange space.
Water cooling heat exchanger bottom in tower reactor 1 is provided with air cooling heat exchanger, air cooling heat exchanger is comprised of two relative orifice plates and the tubulation that is arranged between two orifice plates, between two orifice plates, tubulation outer wall and tower reactor inwall form airtight air heat swapace, hot synthesis gas outlet 6 and cold synthesis gas import 8 are connected with air heat swapace.
In tower reactor, between air inlet 9 and air cooling heat exchanger, gas distributor 10 is installed, gas distributor is orifice plate, and the cylindrical of orifice plate is connected with tower reactor inwall is airtight.
Catalyst 5 is housed in the tubulation of the gentle cold heat exchanger of above-mentioned water cooling heat exchanger.
During use, cold synthesis gas is by being arranged on the cold synthesis gas import 8 of air cooling heat exchanger lower end, enter air heat swapace, upwards flow and absorb after the interior synthetic reaction liberated heat of tubulation, hot synthesis gas outlet 6 by air cooling heat exchanger upper end is flowed out, and by pipeline, enters the air inlet 9 that install tower reactor lower end, the gas distributor 10 being then comprised of orifice plate, after synthesis gas is uniform, enter in the tubulation that catalyst is housed, synthesize reflection.Reacted gas, by spiral gas-liquid-solid separator, will enter next workshop section after gas-liquid-solid separation.
Too high for preventing reaction temperature, the air cooling heat exchanger top in tower reactor, is provided with water cooling heat exchanger, by water cooling, reaction temperature is reduced, the simultaneously absorption of water cooling heat exchanger large quantitative response liberated heat water, can be used as thermal source and use.
As produce 100000 tons of one-step method dimethyl ether synthesis slurry bed reactors per year, structure of reactor: internal diameter 3.2m, high 20m, built-in 400 Φ 38 * 2 heat exchangers, 68 tons of inert heat carrier paraffin oils, 34.46 tons of the difunctional fine granularity catalyst that filling industrial methanol synthetic catalyst and methanol dehydration catalyst form.At 240 ℃ of temperature, pressure 6.0MPa, air speed 1.0L/gh, H
2content 65.77%, CO content 32.84%, CO
2content 1.39%.The conversion ratio 80% of CO, dimethyl ether be selectively 88%, CO
2selective 0.8%, C
2above selective 0.01%.
Comparison example: under identical reaction condition, adopt general bubbling bed reactor, the conversion ratio 75% of CO, dimethyl ether be selectively 85%, CO
2selective 2.3%, C
2above selective 0.03%.
Claims (2)
1. a dimethyl ether synthesis reactor, comprise tower reactor, be arranged on the heat exchanger in tower reactor, it is characterized in that being provided with the gentle cold heat exchanger of water cooling heat exchanger from top to bottom in tower reactor (1), separator (13) is installed in tower reactor upper end, air inlet (9) is installed in tower reactor lower end, gas distributor (10) is installed between air cooling heat exchanger and air inlet in tower reactor, the water inlet (11) and the delivery port (12) that are connected with water cooling heat exchanger are installed on tower reactor, the hot synthesis gas outlet (6) and the cold synthesis gas import (8) that are connected with air cooling heat exchanger are from top to bottom installed on tower reactor, the air inlet (9) that hot synthesis gas outlet (6) is installed with tower reactor lower end by pipeline is connected,
Above-mentioned water cooling heat exchanger forms by being relatively arranged on two orifice plates (4) in tower reactor (1) and the tubulation (2) being arranged between two orifice plates, between two orifice plates, tubulation outer wall and tower reactor inwall form airtight heat exchange space (3), water inlet (11) and delivery port (12) from the bottom to top order are arranged on tower reactor, and are connected with heat exchange space;
Above-mentioned air cooling heat exchanger forms by being relatively arranged on two orifice plates in tower reactor (1) and the tubulation being arranged between two orifice plates, between two orifice plates, tubulation outer wall and tower reactor inwall form airtight air heat swapace, hot synthesis gas outlet (6) and cold synthesis gas import (8) are connected with air heat swapace;
Catalyst (5) is housed in the tubulation of the gentle cold heat exchanger of above-mentioned water cooling heat exchanger.
2. dimethyl ether synthesis reactor according to claim 1, is characterized in that above-mentioned separator (13) is spiral gas-liquid-solid separator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110252753.8A CN102319553B (en) | 2011-08-30 | 2011-08-30 | Dimethyl ether synthesis reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110252753.8A CN102319553B (en) | 2011-08-30 | 2011-08-30 | Dimethyl ether synthesis reactor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102319553A CN102319553A (en) | 2012-01-18 |
| CN102319553B true CN102319553B (en) | 2014-01-29 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201110252753.8A Active CN102319553B (en) | 2011-08-30 | 2011-08-30 | Dimethyl ether synthesis reactor |
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Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE10120801A1 (en) * | 2001-04-27 | 2002-11-07 | Basf Ag | Reactor for gas / liquid or gas / liquid / solid reactions |
| CN2576323Y (en) * | 2002-10-24 | 2003-10-01 | 华东理工大学 | Internal-cooling pipe-casing compound fixed-bed combined catalytic reactor |
| CN102133512B (en) * | 2010-01-21 | 2013-05-15 | 华东理工大学 | Reactor applied to gas-phase exothermic reaction |
| CN102029130B (en) * | 2010-10-27 | 2014-11-05 | 神华集团有限责任公司 | Device and method for preparing dimethyl ether |
| CN202191894U (en) * | 2011-08-30 | 2012-04-18 | 神华宁夏煤业集团有限责任公司 | Dimethyl ether synthesis reactor |
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| CN102319553A (en) | 2012-01-18 |
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Owner name: SHENHUA NINGXIA COAL INDUSTRY GROUP CO., LTD . EAS Free format text: FORMER OWNER: EAST CHINA UNIVERSITY OF SCIENCE AND TECHNOLOGY Effective date: 20130322 Owner name: SHENHUA GROUP CO., LTD. Free format text: FORMER OWNER: SHENHUA NINGXIA COAL INDUSTRY GROUP CO., LTD . Effective date: 20130322 |
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Effective date of registration: 20130322 Address after: 100011 Beijing, Dongcheng District Anwai Binhe West Road No. 22 Shenhua building Applicant after: Shenhua Group LLC Applicant after: Shenhua Ningxia Coal Industry Group Co., Ltd . Applicant after: East China University of Science and Technology Address before: 750002, No. 168 middle Beijing Road, Jinfeng District, the Ningxia Hui Autonomous Region, Yinchuan Applicant before: Shenhua Ningxia Coal Industry Group Co., Ltd . Applicant before: East China University of Science and Technology |
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